CN110577633B - Pretreatment system and method for polycarbonate production raw materials - Google Patents
Pretreatment system and method for polycarbonate production raw materials Download PDFInfo
- Publication number
- CN110577633B CN110577633B CN201910857489.7A CN201910857489A CN110577633B CN 110577633 B CN110577633 B CN 110577633B CN 201910857489 A CN201910857489 A CN 201910857489A CN 110577633 B CN110577633 B CN 110577633B
- Authority
- CN
- China
- Prior art keywords
- pipeline
- valve
- bisphenol
- differential pressure
- flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000004417 polycarbonate Substances 0.000 title claims abstract description 39
- 229920000515 polycarbonate Polymers 0.000 title claims abstract description 36
- 239000002994 raw material Substances 0.000 title claims abstract description 32
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims description 22
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 claims abstract description 154
- ROORDVPLFPIABK-UHFFFAOYSA-N diphenyl carbonate Chemical compound C=1C=CC=CC=1OC(=O)OC1=CC=CC=C1 ROORDVPLFPIABK-UHFFFAOYSA-N 0.000 claims abstract description 55
- 238000003860 storage Methods 0.000 claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 230000003068 static effect Effects 0.000 claims abstract description 9
- 238000002203 pretreatment Methods 0.000 claims abstract description 4
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 19
- 238000002156 mixing Methods 0.000 claims description 8
- 230000001960 triggered effect Effects 0.000 claims description 4
- 238000007664 blowing Methods 0.000 claims description 2
- 238000004140 cleaning Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 238000002161 passivation Methods 0.000 claims description 2
- 238000000354 decomposition reaction Methods 0.000 abstract description 3
- 230000006866 deterioration Effects 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 description 8
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000005809 transesterification reaction Methods 0.000 description 5
- XTBFPVLHGVYOQH-UHFFFAOYSA-N methyl phenyl carbonate Chemical compound COC(=O)OC1=CC=CC=C1 XTBFPVLHGVYOQH-UHFFFAOYSA-N 0.000 description 4
- 238000006068 polycondensation reaction Methods 0.000 description 4
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- JESXATFQYMPTNL-UHFFFAOYSA-N 2-ethenylphenol Chemical compound OC1=CC=CC=C1C=C JESXATFQYMPTNL-UHFFFAOYSA-N 0.000 description 2
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 2
- 238000012696 Interfacial polycondensation Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 150000002148 esters Chemical group 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 230000003287 optical effect Effects 0.000 description 2
- 229920005668 polycarbonate resin Polymers 0.000 description 2
- 239000004431 polycarbonate resin Substances 0.000 description 2
- 238000012827 research and development Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 125000005587 carbonate group Chemical group 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010292 electrical insulation Methods 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
- C08G64/04—Aromatic polycarbonates
- C08G64/06—Aromatic polycarbonates not containing aliphatic unsaturation
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
- C08G64/20—General preparatory processes
- C08G64/205—General preparatory processes characterised by the apparatus used
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
- C08G64/20—General preparatory processes
- C08G64/30—General preparatory processes using carbonates
- C08G64/307—General preparatory processes using carbonates and phenols
Abstract
The invention discloses a pretreatment system and a pretreatment method for polycarbonate production raw materials, wherein the pretreatment system comprises a bisphenol A storage tank, a diphenyl carbonate storage tank, a bisphenol A pipeline and a diphenyl carbonate pipeline; the bisphenol A storage tank is connected to the polycarbonate reaction device through a bisphenol A pipeline, and a static mixer is arranged on the bisphenol A pipeline; the diphenyl carbonate storage tank was incorporated into the bisphenol a line prior to the inlet of the static mixer by a diphenyl carbonate line. The production raw material pretreatment system can avoid the problems of hue and quality deterioration caused by raw material mutual stringing and raw material decomposition, and can greatly improve the quality and quality stability of the polycarbonate product by combining with accurate raw material molar ratio.
Description
Technical Field
The invention relates to the technical field of polycarbonate engineering, in particular to a pretreatment system and a pretreatment method for a polycarbonate production raw material.
Background
Polycarbonate (PC for short) is a high molecular polymer containing carbonate groups in the molecular chain, and is a general engineering plastic with excellent performance, and industrial production is rapidly formed in developed countries since the advent of the polycarbonate, and the technology is continuously developed and the device scale is continuously enlarged. The polycarbonate has the characteristics of good optical transparency, high impact strength, excellent heat stability, creep resistance, cold resistance, electrical insulation, flame retardance and the like, so that the polycarbonate is widely applied to the fields of transparent building boards, electronic appliances, optical disk media, automobile industry and the like. Although the polycarbonate research and development in China is earlier, a plurality of enterprises are involved in research and development production, the production device is small in scale, low in productivity and poor in product quality due to the fact that the process technology is behind, and the domestic enterprises mainly introduce foreign process technology to produce the polycarbonate. Therefore, the development of new technology of the polycarbonate technology is enhanced, the industrialization of the technology is accelerated, the production cost is reduced, the product quality is improved, and the technology becomes an important strategic requirement of polycarbonate production enterprises in China and China.
The current PC production process technology mainly comprises the following steps:
1) An interfacial polycondensation phosgene method;
2) A transesterification melt polycondensation process;
3) The non-phosgene ester exchange melt polycondensation method is developed successfully based on the production process of the ester exchange method because phosgene is not used thoroughly in the process, and belongs to a green and environment-friendly process route. The production process comprises the following two steps: (1) synthesis of diphenyl carbonate (DPC) by transesterification: phenol+dimethyl carbonate (DMC) →dpc; (2) dpc+bisphenol a (BPA) →pc. Firstly, propylene carbonate is subjected to transesterification with methanol to produce dimethyl carbonate (DMC); secondly, phenol and DMC react first to form Methyl Phenyl Carbonate (MPC), then MPC and phenol react further to form DPC, and MPC disproportionates to form DPC. After DPC is synthesized, the DPC and bisphenol A are subjected to transesterification reaction at high temperature and high vacuum in the presence of a trace amount of catalyst to generate an oligomer, and then the oligomer is further subjected to polycondensation to obtain a PC product. Compared with an interfacial polycondensation phosgene method and an ester exchange melt polycondensation method, the method has the following advantages: (1) no toxic phosgene and solvent methylene dichloride are used, no desolventizing and washing desalting procedures are carried out, the flow is simple, and the pollution to the environment is greatly reduced; (2) the byproducts of methanol and phenol can be recycled, so that the raw material cost is reduced.
Since polycarbonate resins have high demands for stability of hue, melt index, and the like, they must be first well controlled in terms of pretreatment of raw materials. In the production process of non-phosgene transesterification melt polymerization method, two main raw materials are bisphenol A and diphenyl carbonate, wherein the melting point of bisphenol A is 157.7 ℃, and bisphenol A is extremely easy to decompose at high temperature, acid and alkali to generate vinyl phenol and phenol, so that the raw materials yellow, and the product quality of polycarbonate resin is further influenced. At present, bisphenol A is granulated first, and liquid diphenyl carbonate heated is sent to a mixing tank with stirring. And then the granular bisphenol A is conveyed to a mixing tank with stirring through air conveying or a bucket elevator to be melted in liquid diphenyl carbonate, and weighing and metering are carried out in the feeding process, so that the mole ratio of the raw materials bisphenol A and the diphenyl carbonate is realized. The melting process requires the jacket steam to continuously provide heat for melting the bisphenol A in solid state, resulting in high energy consumption in production. Meanwhile, the metering precision of the process is low, and the deviation of the molar ratio of the raw material proportion compared with the actual ratio is easy to cause.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a pretreatment system and a pretreatment method for a raw material for producing polycarbonate.
In order to achieve the above object, one technical scheme of the present invention is as follows: a pretreatment system for polycarbonate production raw materials, which is characterized in that: comprises a bisphenol A storage tank, a diphenyl carbonate storage tank, a bisphenol A pipeline, a diphenyl carbonate pipeline, a controller, a first differential pressure transmitter, a second differential pressure transmitter and a flow calculator,
the bisphenol A storage tank is connected to the polycarbonate reaction device through a bisphenol A pipeline, the bisphenol A pipeline is sequentially provided with a first switch valve, a first pressure gauge, a first mass flowmeter, a first flow control valve, a three-way valve, a second switch valve, a first non-return valve, a second pressure gauge, a third pressure gauge and a static mixer from the outlet end of the bisphenol A storage tank to the material inlet end of the polycarbonate reaction device, the inlet and the outlet of the three-way valve are connected with the bisphenol A pipeline, the outlet of the three-way valve is connected with the inlet of the bisphenol A storage tank through a circulating pipeline,
the diphenyl carbonate storage tank is integrated on a bisphenol A pipeline between the first check valve and the second pressure gauge through a diphenyl carbonate pipeline, a third switch valve, a fourth pressure gauge, a second mass flowmeter, a second flow control valve, a fourth switch valve and a second check valve are sequentially arranged at the junction of the diphenyl carbonate pipeline and the bisphenol A pipeline from the outlet end of the diphenyl carbonate pipeline,
the flow calculator is respectively connected with the first mass flowmeter and the second mass flowmeter through signals, the first differential pressure transmitter is respectively connected with the first pressure gauge and the third pressure gauge through signals, the second differential pressure transmitter is respectively connected with the second pressure gauge and the fourth pressure gauge through signals, the controller is respectively connected with the first differential pressure transmitter, the second differential pressure transmitter, the flow calculator, the three-way valve, the second switch valve and the fourth switch valve through signals,
the controller, the first differential pressure transmitter, the second differential pressure transmitter, the flow calculator, the three-way valve, the second switching valve and the fourth switching valve form an interlocking system, and when the differential pressure value of any one of the first differential pressure transmitter and the second differential pressure transmitter is different from a system set value or the flow difference value of the flow calculator is different from the system set value, the interlocking system is triggered, and the controller controls the three-way valve to close the outlet b, open the outlet c, close the second switching valve and close the fourth switching valve.
Further; the first mass flowmeter is in signal connection with the first flow control valve, the second mass flowmeter is in signal connection with the second flow control valve, and the first flow control valve is in signal connection with the second flow control valve.
Further; still include steam pipeline, steam pipeline connects bisphenol A pipeline, and the tie point is located between first ooff valve and the first manometer, steam pipeline is equipped with first stop valve.
Further; still include phenol storage tank and phenol pipeline, the phenol storage tank passes through phenol pipeline connection diphenyl carbonate pipeline, and the tie point is located between third ooff valve and the fourth manometer, be equipped with the second stop valve on the phenol pipeline.
Further; the bisphenol A pipeline, the diphenyl carbonate pipeline, the circulating pipeline and the phenol pipeline are all steam tracing pipelines.
The technical scheme of the invention is as follows: a method for pretreating a polycarbonate production raw material, comprising the steps of:
1) Firstly, setting a first flow control valve flow and a second flow control valve flow according to the feeding mole ratio of bisphenol A to diphenyl carbonate;
2) Opening a first switch valve and a second switch valve, opening an outlet of a three-way valve b, closing an outlet of the three-way valve c, closing a first stop valve, enabling liquid bisphenol A to enter a bisphenol A pipeline, and automatically adjusting the opening of a valve core by a first flow control valve according to a set flow;
3) Opening a third switch valve and a fourth switch valve, closing a second stop valve, enabling liquid diphenyl carbonate to enter a diphenyl carbonate pipeline, automatically adjusting the opening of a valve core by a second flow control valve according to a set flow, merging with liquid bisphenol A, entering a static mixer, fully mixing, and entering a polycarbonate reaction device;
4) The first differential pressure transmitter transmits the differential pressure value between the first pressure gauge and the third pressure gauge to the controller, the second differential pressure transmitter transmits the differential pressure value between the second pressure gauge and the fourth pressure gauge to the controller, and the flow calculator transmits the flow difference value between the first mass flowmeter and the second mass flowmeter to the controller; when the differential pressure value of any one of the first differential pressure transmitter and the second differential pressure transmitter is different from the system set value or the flow difference value of the flow calculator is different from the system set value, triggering interlocking, controlling the outlet of the three-way valve b to be closed and the outlet of the three-way valve c to be opened by the controller, returning bisphenol A to the bisphenol A storage tank through the circulating pipeline, simultaneously controlling the second switching valve to be closed and the fourth switching valve to be closed, and then restarting from the step (2) if the operation is required.
Further; the method further comprises the step 5) of opening a first stop valve after stopping the reaction ending system, introducing steam into a steam pipeline, and blowing the steam into a bisphenol A pipeline; and opening a second stop valve, and cleaning the passivation pipeline by enabling phenol to enter the diphenyl carbonate pipeline.
The invention has the beneficial effects that:
the invention directly mixes liquid diphenyl carbonate and liquid bisphenol A in a pipeline. The temperature of the mixed raw material liquid can be reduced to 140+/-5 ℃, and the thermal stability of the mixed raw material liquid is greatly improved. The flow of liquid bisphenol A is controlled by a flow control valve before mixing to shorten the residence time of liquid bisphenol A. The invention can prevent bisphenol A and diphenyl carbonate from being mixed by arranging the pressure gauge, the mass flowmeter, the flow control valve, the switch valve, the check valve and the interlocking system on the bisphenol A pipeline and the diphenyl carbonate pipeline. Meanwhile, the three-way valve and the circulating pipeline are arranged on the bisphenol A pipeline, so that liquid bisphenol A in the pipeline can be returned to the bisphenol A storage tank when interlocking occurs, and the retention, decomposition and deterioration are avoided.
The invention carries out liquid transportation and mixing of bisphenol A and diphenyl carbonate. The flow control valve can accurately control the mole ratio of the raw materials, solves the defects of high energy consumption and poor mole ratio precision in the traditional raw material treatment, and simultaneously solves the waste gas treatment problem caused by the traditional stirring tank mixing mode.
The production raw material pretreatment system can avoid the problems of hue and quality deterioration caused by raw material mutual stringing and raw material decomposition, and can greatly improve the quality and quality stability of the polycarbonate product by combining with accurate raw material molar ratio.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
fig. 2 is a control block diagram of the linkage system of the present invention.
In the figure: 1. a first switching valve; 2. a first pressure gauge; 3. a first mass flow meter; 4. a first flow control valve; 5. a three-way valve; 6. a second switching valve; 7. a first non-return valve; 8. a second pressure gauge; 9. a third pressure gauge; 10. a static mixer; 11. a first stop valve; 12. a third switching valve; 13. a fourth pressure gauge; 14. a second mass flow meter; 15. a second flow control valve; 16. a fourth switching valve; 17. a second non-return valve; 18. a second shut-off valve; 19. a first differential pressure transmitter; 20. a second differential pressure transmitter; 21. a flow rate calculator; l1, bisphenol a line; l2, diphenyl carbonate line; l3, steam line; l4, phenol line; l5, a circulating pipeline.
Detailed Description
Examples:
as shown in fig. 1 and 2, a polycarbonate production raw material pretreatment system comprises a bisphenol a storage tank, a diphenyl carbonate storage tank, a polycarbonate reaction device, a steam pipeline L3, a phenol storage tank, a phenol pipeline L4, a bisphenol a pipeline L1, a diphenyl carbonate pipeline L2, a controller, a first differential pressure transmitter 19, a second differential pressure transmitter 20 and a flow calculator 21.
The bisphenol A storage tank is connected with the polycarbonate reaction device through a bisphenol A pipeline L1, the bisphenol A pipeline L1 is sequentially provided with a first switch valve 1, a first pressure gauge 2, a first mass flowmeter 3, a first flow control valve 4, a three-way valve 5, a second switch valve 6, a first check valve 7, a second pressure gauge 8, a third pressure gauge 9 and a static mixer 10 from the outlet end of the bisphenol A storage tank to the feeding port end of the polycarbonate reaction device, the inlet and the outlet of the three-way valve 5 are connected with the bisphenol A pipeline L1, and the outlet of the three-way valve 5 is connected with the inlet of the bisphenol A storage tank through a circulating pipeline L5.
The diphenyl carbonate storage tank is integrated onto a bisphenol A pipeline L1 between a first check valve 7 and a second pressure gauge 8 through a diphenyl carbonate pipeline L2, and a third switch valve 12, a fourth pressure gauge 13, a second mass flowmeter 14, a second flow control valve 15, a fourth switch valve 16 and a second check valve 17 are sequentially arranged at the junction of the diphenyl carbonate pipeline L2 from the outlet end of the diphenyl carbonate to the bisphenol A pipeline L1.
The steam pipeline L3 is connected with the bisphenol A pipeline L1, the connection point is positioned between the first switch valve 1 and the first pressure gauge 2, and the steam pipeline L3 is provided with a first stop valve 11.
The phenol storage tank is connected with a diphenyl carbonate pipeline L2 through a phenol pipeline L4, the connection point is positioned between the third switch valve 12 and the fourth pressure gauge 13, and a second stop valve 18 is arranged on the phenol pipeline L4.
The bisphenol A pipeline L1, the diphenyl carbonate pipeline L2, the circulating pipeline L5 and the phenol pipeline L4 are steam tracing pipelines.
The first mass flowmeter 3 is in signal connection with the first flow control valve 4, the second mass flowmeter 14 is in signal connection with the second flow control valve 15, the first flow control valve 4 is in signal connection with the second flow control valve 15, the flow calculator 21 is respectively connected with the first mass flowmeter 3 and the second mass flowmeter 14 through signals, and the first flow control valve 4 and the second flow control valve 15 can automatically adjust the opening degree of the valve core according to set flow.
The first differential pressure transmitter 19 is respectively connected with the first pressure gauge 2 and the third pressure gauge 9 through signals, the second differential pressure transmitter 20 is respectively connected with the second pressure gauge 8 and the fourth pressure gauge 13 through signals, and the controller is respectively connected with the first differential pressure transmitter 19, the second differential pressure transmitter 20, the flow calculator 21, the three-way valve 5, the second switch valve 6 and the fourth switch valve 16 through signals.
The controller, the first differential pressure transmitter 19, the second differential pressure transmitter 20, the flow calculator 21, the three-way valve 5, the second switch valve 6 and the fourth switch valve 16 form an interlocking system, and when the differential pressure value of any one of the first differential pressure transmitter 19 and the second differential pressure transmitter 20 is different from a system set value or the flow difference value of the flow calculator 21 is different from the system set value, the interlocking is triggered, and the controller controls the three-way valve 5b to close the outlet, the outlet of the three-way valve c to open, and the second switch valve 6 and the fourth switch valve 16 to close.
A method for pretreating a polycarbonate production raw material, comprising the steps of:
1) Firstly, respectively setting the flow of a first flow control valve 4 and a second flow control valve 15 according to the feeding mole ratio of bisphenol A to diphenyl carbonate of 1:1; the first flow control valve 4 may receive a flow signal of the first mass flowmeter 3 and perform flow indication control integration (FICQ); the second flow control valve 15 may receive the flow signal of the second mass flowmeter 14 and perform flow indication integration (FIQ) and calculate a flow ratio (FFC) with the first flow control valve 4;
2) Opening the first switch valve 1 and the second switch valve 6, opening the outlet of the three-way valve 5b, closing the outlet of the three-way valve c, closing the first stop valve 11, allowing liquid bisphenol A to enter the bisphenol A pipeline L1, and automatically regulating the opening of the valve core by the first flow control valve 4 according to the set flow;
3) Opening the third switch valve 12 and the fourth switch valve 16, closing the second stop valve 18, enabling liquid diphenyl carbonate to enter a diphenyl carbonate pipeline L2, automatically adjusting the opening of a valve core by the second flow control valve 15 according to the set flow, merging with liquid bisphenol A, entering the static mixer 10, fully mixing, and entering a polycarbonate reaction device;
4) The first differential pressure transmitter 19 calculates a differential pressure value between the first pressure gauge 2 and the third pressure gauge 9 and transmits the differential pressure value to the controller, the second differential pressure transmitter 20 calculates a differential pressure value between the second pressure gauge 8 and the fourth pressure gauge 13 and transmits the differential pressure value to the controller, and the flow calculator 21 calculates a flow difference value between the first mass flowmeter 3 and the second mass flowmeter 14 and transmits the flow difference value to the controller. When the differential pressure value of any one of the first differential pressure transmitter 19 and the second differential pressure transmitter 20 is different from the system set value or the differential flow value of the flow calculator 21 is different from the system set value, the interlocking is triggered, and an interlocking signal 1-01 is sent to the controller, the controller controls the three-way valve 5b to be closed and the three-way valve 5 c to be opened, bisphenol A is returned to the bisphenol A storage tank through the circulating pipeline L5, and simultaneously controls the second switching valve 6 to be closed and the fourth switching valve 16 to be closed, and then the operation can be restarted from the step (2) if required;
5) After the reaction is stopped, the first stop valve 11 is opened, steam is introduced into the steam pipeline L3, and the steam enters the bisphenol A pipeline L1 for purging; the second shut-off valve 18 was opened and phenol was introduced into the diphenyl carbonate line L2 to clean the passivated line.
The above-described embodiments are merely preferred embodiments of the present invention, and the present invention is not limited in any way, and other variations and modifications may be made without departing from the technical aspects set forth in the claims.
In the description of the present invention, it should be understood that the terms "orientation" or "positional relationship" are based on the orientation or positional relationship shown in the drawings, and are merely for convenience of description and to simplify the description, rather than to indicate or imply that the apparatus or elements referred to must have a particular orientation, be constructed and operate in a particular orientation, and therefore should not be construed as limiting the invention.
Claims (5)
1. A pretreatment system for polycarbonate production raw materials, which is characterized in that: comprises a bisphenol A storage tank, a diphenyl carbonate storage tank, a bisphenol A pipeline, a diphenyl carbonate pipeline, a controller, a first differential pressure transmitter, a second differential pressure transmitter and a flow calculator,
the bisphenol A storage tank is connected to the polycarbonate reaction device through a bisphenol A pipeline, the bisphenol A pipeline is sequentially provided with a first switch valve, a first pressure gauge, a first mass flowmeter, a first flow control valve, a three-way valve, a second switch valve, a first non-return valve, a second pressure gauge, a third pressure gauge and a static mixer from the outlet end of the bisphenol A storage tank to the material inlet end of the polycarbonate reaction device, the inlet and the outlet of the three-way valve are connected with the bisphenol A pipeline, the outlet of the three-way valve is connected with the inlet of the bisphenol A storage tank through a circulating pipeline,
the diphenyl carbonate storage tank is integrated on a bisphenol A pipeline between the first check valve and the second pressure gauge through a diphenyl carbonate pipeline, a third switch valve, a fourth pressure gauge, a second mass flowmeter, a second flow control valve, a fourth switch valve and a second check valve are sequentially arranged at the junction of the diphenyl carbonate pipeline and the bisphenol A pipeline from the outlet end of the diphenyl carbonate pipeline,
the flow calculator is respectively connected with the first mass flowmeter and the second mass flowmeter through signals, the first differential pressure transmitter is respectively connected with the first pressure gauge and the third pressure gauge through signals, the second differential pressure transmitter is respectively connected with the second pressure gauge and the fourth pressure gauge through signals, the controller is respectively connected with the first differential pressure transmitter, the second differential pressure transmitter, the flow calculator, the three-way valve, the second switch valve and the fourth switch valve through signals,
the controller, the first differential pressure transmitter, the second differential pressure transmitter, the flow calculator, the three-way valve, the second switching valve and the fourth switching valve form an interlocking system, when the differential pressure value of any one of the first differential pressure transmitter and the second differential pressure transmitter is different from a system set value or the flow difference value of the flow calculator is different from the system set value, the interlocking is triggered, and the controller controls the three-way valve to be closed at the outlet of b, open at the outlet of c, closed at the second switching valve and closed at the fourth switching valve;
the first mass flowmeter is in signal connection with the first flow control valve, the second mass flowmeter is in signal connection with the second flow control valve, and the first flow control valve is in signal connection with the second flow control valve;
still include steam pipeline, steam pipeline connects bisphenol A pipeline, and the tie point is located between first ooff valve and the first manometer, steam pipeline is equipped with first stop valve.
2. The polycarbonate production raw material pretreatment system according to claim 1, wherein:
still include phenol storage tank and phenol pipeline, the phenol storage tank passes through phenol pipeline connection diphenyl carbonate pipeline, and the tie point is located between third ooff valve and the fourth manometer, be equipped with the second stop valve on the phenol pipeline.
3. The polycarbonate production raw material pretreatment system according to claim 2, wherein: the bisphenol A pipeline, the diphenyl carbonate pipeline, the circulating pipeline and the phenol pipeline are all steam tracing pipelines.
4. A method of pretreatment of a polycarbonate production raw material pretreatment system according to claim 3, comprising the steps of:
1) Firstly, setting a first flow control valve flow and a second flow control valve flow according to the feeding mole ratio of bisphenol A to diphenyl carbonate;
2) Opening a first switch valve and a second switch valve, opening an outlet of a three-way valve b, closing an outlet of the three-way valve c, closing a first stop valve, enabling liquid bisphenol A to enter a bisphenol A pipeline, and automatically adjusting the opening of a valve core by a first flow control valve according to a set flow;
3) Opening a third switch valve and a fourth switch valve, closing a second stop valve, enabling liquid diphenyl carbonate to enter a diphenyl carbonate pipeline, automatically adjusting the opening of a valve core by a second flow control valve according to a set flow, merging with liquid bisphenol A, entering a static mixer, fully mixing, and entering a polycarbonate reaction device;
4) The first differential pressure transmitter transmits the differential pressure value between the first pressure gauge and the third pressure gauge to the controller, the second differential pressure transmitter transmits the differential pressure value between the second pressure gauge and the fourth pressure gauge to the controller, and the flow calculator transmits the flow difference value between the first mass flowmeter and the second mass flowmeter to the controller; when the differential pressure value of any one of the first differential pressure transmitter and the second differential pressure transmitter is different from a system set value or the flow difference value of the flow calculator is different from the system set value, the controller triggers the interlocking, controls the outlet of the three-way valve b to be closed, the outlet of the three-way valve c to be opened, bisphenol A returns to the bisphenol A storage tank through the circulating pipeline, and simultaneously controls the second switch valve to be closed and the fourth switch valve to be closed.
5. The pretreatment method of a pretreatment system for polycarbonate production raw materials according to claim 4, wherein: the method further comprises the step 5) of opening a first stop valve after stopping the reaction ending system, introducing steam into a steam pipeline, and blowing the steam into a bisphenol A pipeline; and opening a second stop valve, and cleaning the passivation pipeline by enabling phenol to enter the diphenyl carbonate pipeline.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910857489.7A CN110577633B (en) | 2019-09-11 | 2019-09-11 | Pretreatment system and method for polycarbonate production raw materials |
| PCT/CN2019/120111 WO2021047037A1 (en) | 2019-09-11 | 2019-11-22 | System and method for pretreating raw materials for polycarbonate production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910857489.7A CN110577633B (en) | 2019-09-11 | 2019-09-11 | Pretreatment system and method for polycarbonate production raw materials |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110577633A CN110577633A (en) | 2019-12-17 |
| CN110577633B true CN110577633B (en) | 2023-12-19 |
Family
ID=68812807
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910857489.7A Active CN110577633B (en) | 2019-09-11 | 2019-09-11 | Pretreatment system and method for polycarbonate production raw materials |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN110577633B (en) |
| WO (1) | WO2021047037A1 (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0306838A2 (en) * | 1987-09-05 | 1989-03-15 | Idemitsu Petrochemical Co. Ltd. | Process of preparing polycarbonates |
| CN104169326A (en) * | 2012-03-30 | 2014-11-26 | 三菱化学株式会社 | Process for manufacturing aromatic polycarbonate and manufacturing facility |
| CN106985300A (en) * | 2017-04-24 | 2017-07-28 | 宁波浙铁大风化工有限公司 | A kind of makrolon preparation system |
| CN211111819U (en) * | 2019-09-11 | 2020-07-28 | 利华益维远化学股份有限公司 | Polycarbonate raw materials for production preliminary treatment system |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6887969B2 (en) * | 2002-10-04 | 2005-05-03 | General Electric Company | Method and apparatus to make high molecular weight melt polycarbonate |
| EP1657272B2 (en) * | 2003-08-21 | 2020-04-08 | Mitsubishi Chemical Corporation | Process for producing aromatic polycarbonate |
| CN105175705A (en) * | 2015-10-15 | 2015-12-23 | 宁波浙铁大风化工有限公司 | Preparation device of polycarbonate |
| CN109265670A (en) * | 2018-08-03 | 2019-01-25 | 宁波浙铁大风化工有限公司 | A kind of preparation process of polycarbonate |
-
2019
- 2019-09-11 CN CN201910857489.7A patent/CN110577633B/en active Active
- 2019-11-22 WO PCT/CN2019/120111 patent/WO2021047037A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0306838A2 (en) * | 1987-09-05 | 1989-03-15 | Idemitsu Petrochemical Co. Ltd. | Process of preparing polycarbonates |
| CN104169326A (en) * | 2012-03-30 | 2014-11-26 | 三菱化学株式会社 | Process for manufacturing aromatic polycarbonate and manufacturing facility |
| CN106985300A (en) * | 2017-04-24 | 2017-07-28 | 宁波浙铁大风化工有限公司 | A kind of makrolon preparation system |
| CN211111819U (en) * | 2019-09-11 | 2020-07-28 | 利华益维远化学股份有限公司 | Polycarbonate raw materials for production preliminary treatment system |
Non-Patent Citations (3)
| Title |
|---|
| 俞金寿 等.化工自动化及仪表.华东理工大学出版社,2011,(第1版),第273-276页. * |
| 匡永泰 等.石油化工安全评价技术.中国石化出版社,2005,(第1版),第278-180页. * |
| 李希 等.涤纶生产仪表及自动化.东南大学出版社,1992,(第1版),第173-175页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2021047037A1 (en) | 2021-03-18 |
| CN110577633A (en) | 2019-12-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102516518B (en) | Method of preparing polycarbonate | |
| CN103059550A (en) | Polyphenylene oxide/polystyrene blend alloy material, its preparation method and application | |
| CN103421298A (en) | Polyphenyl ether / polystyrene blending alloy material and preparation method thereof | |
| CN101089046A (en) | Transparent polycarbonate alloy composite material and its prepn process | |
| CN106947226A (en) | A kind of PET composite material | |
| CN211111819U (en) | Polycarbonate raw materials for production preliminary treatment system | |
| EP2762516B1 (en) | Polycarbonate and method for preparing same | |
| CN110577633B (en) | Pretreatment system and method for polycarbonate production raw materials | |
| KR101211979B1 (en) | Process for production of polycarbonate resin | |
| JP2000178354A (en) | Production of aromatic polycarbonate | |
| EP1691959A2 (en) | A process for the introduction of additives, into polymer melts | |
| CN102295826A (en) | Reinforced flame-retarding polyethylene glycol terephthalate blended material | |
| CN108789913B (en) | Raw material mixing device and mixing process for continuously producing polycarbonate | |
| CN103476558A (en) | Polycarbonate-resin manufacturing method | |
| CN115850944B (en) | High-light-transmittance thin-wall flame-retardant polycarbonate composition and preparation method thereof | |
| CN105175706A (en) | High-light-permeability panlite and production method thereof | |
| CN101668792B (en) | Method for production of aromatic polycarbonate resin composition | |
| KR101741280B1 (en) | Polycarbonate resin composition | |
| JP3783921B2 (en) | Method for producing aromatic polycarbonate | |
| CN204352787U (en) | One is dyed cloth additive compound system | |
| CN109294198B (en) | Preparation method and application of transparent high-temperature-resistant polyarylate/polycarbonate alloy ester exchange reaction inhibitor | |
| CN111892804A (en) | Ultrahigh-hardness high-transparency PC material and preparation method thereof | |
| CN102532503B (en) | Preparation method of polycarbonate | |
| CN101125918B (en) | Neutralization treatment method for catalyst used for preparing polycarbonate from aromatics dihydroxy compounds and diester carbonate, and neutralizing agent used for the same | |
| CN103642012A (en) | Method for preparing high-flow and high-modulus polybutylene terephthalate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |